Turbine oil production
CROSS REFERENCE TO RELATED APPLICATIONS 
     This application is a continuation in part of prior co-pending application Ser. No. 081,935, filed Aug. 5, 1987 and now abandoned, which is incorporated herein by reference. 
    
    
     FIELD OF THE INVENTION 
     The present invention relates to a process for the production of machine oils. 
     BACKGROUND OF THE INVENTION 
     Mineral oil lubricants including turbine oils are derived from various crude oil stocks by a variety of refining processes. Generally, these refining processes are directed towards obtaining a lubricant base stock of suitable boiling point, viscosity, viscosity index (VI) and other characteristics. Generally, the base stock will be produced from the crude oil by distillation of the crude in atmospheric and vacuum distillation towers, followed by the separation of undesirable aromatic components and finally, by dewaxing and various finishing steps. Because aromatic components lead to high viscosity and extremely poor viscosity indices, as well as poor oxidation stability in the finished product, the use of asphaltic type crudes is not preferred as the yield of acceptable lube stocks will be extremely low after the large quantities of aromatic components contained in such crudes have been separated out; paraffinic and naphthenic crude stocks will therefore be preferred but aromatic separation procedures will still be necessary in order to remove undesirable aromatic components. In the case of the lubricant distillate fractions, generally referred to as the neutrals, e.g., heavy neutral, light neutral, etc., the aromatics will be extraced by solvent extraction using a solvent such as furfural, N-methyl-2-pyrrolidone, phenol or another material which is selective for the extraction of the aromatic components. If the lube stock is a residual lube stock, the asphaltenes will first be removed in a propane deasphalting step followed by solvent extraction of residual anomatics to produce a lube generally referred to as bright stock. In either case, however, a dewaxing step is normally necessary in order for the lubricant to have a satisfactorily low pour point and cloud point, so that it will not solidify or precipitate the less soluble paraffinic components under the influence of low temperatures. 
     A number of dewaxing processes are known in the petroleum refining industry and of these, solvent dewaxing with solvents such as xethylethylketone (MEK), a mixture of MEK and toluene or liquid propane, has been the one which has achieved the widest use in the industry. Recently, however, proposals have been made for using catalytic dewaxing processes for the production of lubricating oil stocks and these processes posses a number of advantages over the conventional solvent dewaxing procedures. The catalytic dewaxing processes which have been proposed are generally similar to those which have been proposed for dewaxing the middle distillate fractions such as heating oils, jet fuels and kerosenes, of which a number have been disclosed in the literature, for example, in Oil and Gas Journal, Jan. 6, 1975, pp. 69-73 and U.S. Pat. Nos. Re. 28,398, 3,956,102 and 4,100,056. Generally, these processes operate by selectively cracking the normal and slightly branched paraffins to produce lower molecular weight products which may then be removed by distillation from the higher boiling lube stock. The catalysts which have been proposed for this purpose have usually been zeolites which have a pore size which admits the straight chain, waxy n-paraffins either alone or with only slightly branched chain paraffins but which exclude more highly branched materials and cycloaliphatics. Zeolites such as ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-38 and the synthetic ferrierites have been proposed for this purpose in dewaxing processes, as described in U.S. Pat. Nos. 3,700,585 (Re. 28398); 3,984,938; 3,933,974; 4,176,050; 4,181,598; 4,222,855; 4,259,170; 4,229,282; 4,251,499; 4,343,692, and 4,247,388. A dewaxing process employing synthetic offretite is described in U.S. Pat. No. 4,259,174. Processes of this type have become commercially available as shown by the 1986 Refining Process Handbook, Hydrocarbon Processing, September 1986, which refers to the availability of the Mobil Lube Dewaxing Process (MLDW). Reference is made to these disclosures for a description of various catalytic dewaxing processes. 
     Although these catalytic dewaxing processes are invariably carried out in the presence of hydrogen, it is not necessary for the stoichiometry of the dewaxing process which, as noted above, proceeds by a shape-selective cracking mechanism. For this reason it is not necessary for the catalyst to include a hydrogenation component although one may be included in order to improve catalyst reactivation. The hydrogen serves to extend catalyst life during each dewaxing cycle. The effluent from the dewaxing reactor includes olefins which have been produced by the cracking reactions and in order to stabilize the product, a hydrotreating step is carried out after the dewaxing to saturate lube boiling range olefins and, depending upon the hydrotreating conditions, to saturate aromatics remaining in the product stream as well as to remove heteroatom impurities, principally sulfur and nitrogen and various color bodies. A process for hydrotreating a catalytically dewaxed lube product is described in U.S. Pat. No. 4,181,598. 
     Turbine oils are a special class of lubricants which require exceptional oxidation stability over extended periods of time. 
     The exceptionally stringent product specifications associated with turbine oils are necessary because of the severe conditions associated with their use. Turbine oils are expected to last the life of the turbine. This involves years of continuous operation at moderately elevated temperature, and in the presence of air, water and metals. The conditions are not at all like those in an automobile. Good survey articles on the special problems of turbine oils are presented in: 
     1. Control of Iurbine Oil Degradation During Use, M. J. Den Herder and P. C. Vienna, Lubrications Engineering, 37 (2), February 1981, and 
     2. Evaluation and Performance of Turbine Oils, G. H. von Fuchs et al, Industrial and Engineering Chemistry, Vbl. 13, No. 15, both of which are incorporated by reference. 
     An additional indication of the severe uses to which turbine oils are put may be taken from the following standardized test methods used to define good turbine oil properties. 
     TOST TEST 
     The Iurbine Oil Stability Test (TCST) modified ASIMD 943 determines the oxidation stability of steam-turbine oils. Briefly, 300 ml of the oil sample is subjected to a temperature of 95° C. in the presence of 60 ml of water, oxygen at a flow rate of 3 liters per hour (plus or minus 1/2 liter per hour) and an iron-copper catalyst. 
     The TOST test is a long term measure of the oxidation stability of the oil. A somewhat related test is JISK 2515; testing method for oxidation characteristics of turbine oils. In this test oxygen is blown into a sample at 95° C. in the presence of steel wire, copper wire and water to observe surface changes in the metals and state of water and oil phases. More details about this and related test methods are contained in U.S. Pat. Nos. 4,247,414 and 4,247,415 which are incorporated herein by reference. 
     RBOT TEST 
     The rotary bomb oxidation test (RBOT) is a relatively short term test method for the oxidation stability of lubricating oils. 
     The RBOT test is a rapid means of estimating the oxidation stability of new turbine oils. In the test, the turbine oil sample, water and a copper catalyst coil are placed in a covered glass container, and placed in a bomb equipped with a pressure gauge. The bomb is charged with oxygen to a pressure of 90 psi (620 kpa) and placed in a constant temperature oil bath maintained at 150° C. and rotated at 100 rpm. The pressure in the bomb is monitored continuously. At first the pressure increases sharply, typically to about 190-200 psi, because of the increase in temperature. The pressure remains relatively stable, until the oil breaks down. The bomb life of the sample is the time in minutes from the start of the test to a 25 psi pressure drop from the established plateau pressure. Usually the test uses a 3 m length of 14 Awg of copper wire which has been cleaned (preferably in sodium cyanide). 
     In general terms the required properties of turbine oils are as follows: 
     Boiling range=650°-1100° F. 
     Viscosity=150-500 SUS at 100° F. 
     Pour Point=+20° F. or less 
     Cloud Point=Preferably no more than 10° F. above pour point 
     Aromatics=less than 5 wt. % 
     Sulfur=less than 10 ppm 
     Nitrogen=less than 2 ppm 
     The viscosity limit set forth above is not a real upper limit. Viscosities higher than this are not normally required for land based turbines, but could find other applications. 
     In contrast, passenger car motor oils will have typical aromatic levels of 20-30 wt. %, sulfur contents of 0.5-1 wt. % and nitrogen contents of 40-60 ppm. With these motor oils specifications as a background, the unusual processing steps needed to meet turbine oil specifications will now be reviewed. 
     Turbine oils must contain very low levels of aromatic components and conventionally are produced by a refining process which includes a severe solvent extraction with a final hydrotreating or hydrofinishing step to reduce the aromatic content to a low level. In order to maximize aromatic saturation the hydrotreating is carried out at high pressure, typically at pressures above 1500 psig (about 10445 kPa abs), usually at 2000-2500 psig (about 13890-17340 kPa abs), over a catalyst comprising a hydrogenation function on a non-acidic support. Following the hydrotreatment, residual aromatic content is usually below about 5 weight percent of the lubricant. 
     One problem which arises with the hydrotreating is that the viscosity of the oil is reduced to a significant extent. This is not unexpected because the relatively viscous aromatics are converted to less viscous naphthenes as a result of the hydrogenation. This viscosity loss means that the more viscous turbine oils have to be produced by distilling deeper into the vacuum residuum i.e., by increasing the end point of the highest boiling distillate fraction. Because this necessitates significant changes in standard operating procedures it is desirably to be avoided. It also implies that the fractions which are of light neutral quality upon vacuum fractionation e.g. 100 SUS at 40° C., are somewhat below target viscosity at the end of the refining process and therefore cannot be used as turbine oils. It would therefore be desirable to control the viscosity of the hydrotreated turbine oil product. 
     Another problem encountered in producing a satisfactory turbine oil is achieving a product which meets both the pour point specification and the cloud point specification. This is not a problem when solvent dewaxing technology is used to achieve specification pour point. When modern, energy efficient catalytic hydrodewaxing is used, some turbine oils exhibit a cloud point which is unacceptably high relative to the pour point. 
     The cloud point problem encountered when using catalytically hydrodewaxed oils can be overcome to some extent by increasing the severity of the dewaxing reaction (and consequently reducing yields) or by a subsequent wax hydroisomerization process using a zeolite beta catalyst, which reduces yields some, but not as much as catalytic hydrodewaxing using a shape selective zeolite. It also may be possible to reduce cloud point by resorting to various additive materials, but use of such additives increases the cost of the turbine oils, and adds some uncertainties about their long term stability. 
     Accordingly it can be seen that turbine oils, and their method of manufacture, present unique problems. Severe hydrotreating to meet the aromatics specification causes loss in viscosity. Catalytic hydrodewaxing to meet pour point causes cloud point problems. There is a need in the industry to develop a more efficient process for producing turbine oils in good yields, with high enough viscosity, and with a satisfactory cloud point. 
     Solvent dewaxing produces a product which is satisfactory both as to pour point and as to cloud point, but solvent dewaxing is expensive and the yields are not as high as desired. 
     Catalytic hydrodewaxing is the preferred method of wax removal for turbine oils, and a good many other oils, but the need to make a satisfactorily low cloud point forces the process to be run at a higher severity than would be required to make a suitable pour point material. 
     Finally, the high pressure hydrotreating associated with modern turbine oil production methods results in a significant loss in viscosity of the hydrotreated turbine oil product, so a away is needed to overcome this deficiency as well. 
     A way has now been discovered to overcome the deficiencies of the prior art methods of producing turbine oil. 
     SUMMARY OF THE INVENTION 
     We have now found that high quality turbine oils may be prepared by a refining process which includes solvent extraction and hydrotreating to remove undesirable aromatic components coupled with dewaxing to improve fluidity characteristics and treatment with an organic peroxide to modify viscosity characteristics and improve the cloud point without, at the same time, significantly changing product viscosity index or fluidity properties. 
     According to the present invention there is therefore provided a process for producing a turbine oil of controlled viscosity, viscosity index and fluidity characteristics by subjecting a distillate lubricating oil fraction to solvent extraction to remove aromatic components, to dewaxing by a solvent or catalytic dewaxing process or both, hydrotreating the dewaxed product to saturate residual aromatics and remove heteroatom-containing impurities and by treatment with an organic peroxide to control the viscosity of the hydrotreated product. The peroxide treatment may take place before or after the hydrotreating step. If desired, a second dewaxing step may be carried out after the peroxide treatment to produce very low pour point products comparable to synthetic lubricants. 
     The use of the peroxide treatment enables the viscosity loss resulting from high pressure hydrotreating to be recovered and permits heavy neutral and higher viscosity products to be produced from a light neutral distillate. 
    
    
     DETAILED DESCRIPTION 
     The present turbine oil refining process is generally applicable to the production of low pour point turbine oil products from lube range hydrocarbon feeds. As such, the feed will generally have an initial boiling point of at least 650° F. (about 345° C.) in order to prevent excessive volatilisation during use. Generally, the end point of the feed will be in the range of 750° F. (about 400° C.) to about 1050° F. (about 565° C.) since distillate (neutral quality) stocks are generally necessary for turbine oil production because of their low aromatic content. The end point of the feed is not in itself significant although the presence of large amounts of high boiling, unextracted residual type material will generally be undesirable because of their effect on the final lubricant properties and because of yield losses which ensure from their removal during refining. 
     The present process may be used with neutral lube feeds ranging from light neutrals, e.g., from 100 SUS at 100° F. to heavy neutrals, e.g., 700 SUS at 100° F. Typical light to medium neutral stocks may have an IBP below 650° F. (about 345° C.) (ASIM D-2887) and the end point may be below 1000° F. (about 540° C.). Heavier neutrals will generally boil in the range 650° C.-1050° F. (about 345°-565° C., ASIM D-1160, 10 mm. Hg), typically from 750° to 1050° F. (about 400°-565° C., ASTM D-1160). 
     The selected distillate fraction is first subjected to solvent extraction to remove undesirable aromatic components using a solvent such as phenol, furfural or N-methylpyrrolidone which is selective for aromatics removal from lube range streams. The degree of extraction should be severe in order to effect a high degree of aromatics removal and conditions in the extraction process adjust accordingly, depending on the feedstock characteristics, the solvent being used, the equipment and the desired product properties. With furfural as the selected solvent, solvent:oil ratios from about 1:1 to 5:1, usually 1:1 to 3:1 at temperatures from about 50° to 200° C., preferably about 80° to 150° C., will be typical. 
     Following the solvent extraction, the raffinate is dewaxed to improve its fluidity properties, especially its pour point, freeze point and cloud point. The dewaxing may be by conventional solvent type processes such as MEK/toluene dewaxing or propane dewaxing or by catalytic dewaxing, preferably using a shape-selective intermediate pore size zeolite such as ZSM-5 or ZSM-23. Dewaxing processes of this kind are well known and are described, for example in the references mentioned above. See also Industrial Application of Shape-Selective Catalysis, Chen and Garwood Catal. Rev. - Sci. Eng. 28 (2-3), 185-264 (1986), especially 244-247, to which reference is made for a description of the preferred lube dewaxing process using a ZSM-5 dewaxing catalyst. A combination of solvent and catalytic dewaxing steps is desirable in that solvent dewaxing can be used to reduce the pour point of the oil to an intermediate level while producing wax as a useful by-product after which catalytic dewaxing may be used to reduce the pour point to very low levels. 
     As described in the Chen and Garwood article, the shape-selective dewaxing over the intermediate pore size zeolite is followed by a hydrotreating step to ensure that the lube meets quality and performance specifications. See also Oil Gas Journal 78 (21), 75 (1980) and U.S. Pat. Nos. 4,181,598 and 4,137,148. The hydrotreating or hydrofinishing step saturates olefins in the lube boiling range and, under high hydrogen pressures, also saturates residual aromatics which have not been removed during the solvent extraction. Ib achieve this, relatively high hydrogen pressures usually at least 1500 psig (about 10,445 kPa) are necessary. The catalyst will typically include a base metal hydrogenation component on a relatively non-acidic porous oxide support such as alumina, silica or silica-alumina. The use of noble metals such as platinum is not excluded except mainly on the grounds of cost and a mild degree of acidity or the support may be desirable to promote ring opening reactions. Base metals of Groups VIA an VIIIA (IUPAC Table) such as nickel, cobalt, molybdenum and vanadium are preferred especially in combinations such as nickel-molybdenum, cobalt-molybdenum. The amount of the metal component is typically up to 20 weight percent of the catalyst, usually 5-20 weight percent. Hydrotreating temperatures are typically about 500° to 800° F. (about 260° to 425° C.), usually 600° to 750° F. (about 315° to 400° C.), with space velocities of 0.1-5, usually 0.1-2 hr -1  LHSV. 
     Peroxide Treatment 
     The dewaxed product is subjected to treatment with an organic peroxide compound at elevated temperature in order to affect a coupling between the paraffinic components (paraffin molecules and alkyl side chains on ring compounds) to increase the viscosity of the lubricant. 
     The preferred class of peroxides which are used are the ditertiary alkyl peroxides represented by the formula ROOR 1  where R &amp; R 1  are the same or different tertiary alkyl radicals preferably lower (C 4  to C 6 ) tertiary alkyl radicals. Suitable peroxides of this kind include ditertiary butyl peroxide, ditertiary amyl peroxide and tertiary butyl, tertiary amyl peroxide. Other organic peroxides may also be used including dialkyl peroxides with one to ten carbon atoms such as dimethyl peroxide, diethyl peroxide, dipropyl peroxide, di-n-butyl peroxide, dihexyl peroxide and acetylperoxides such as dibenzoylperoxide. 
     The amount of peroxy compound used in the process is determined by the increase in viscosity which is desired in the treatment. In general, the increase in viscosity is related to the amount of peroxide used with greater increases resulting from greater -amounts of peroxide. As a general guide, the amount of peroxide catalyst employed will be from 1 to 50, preferably from 4 to 30 weight percent of the oil. There is essentially an exponential relationship between the proportion of peroxide used and the viscosity increase, both with batch and continuous reaction. The presence of hydrogen may decrease peroxide utilisation slightly but significant increases in viscosity may still be obtained without other lube properties (pour point, V.I.) being significantly affected. It would therefore be practicable to cascade the effluent from a catalytic hydrodewaxing/hydrotreating unit directly to a peroxide treatment reactor, permitting the hydrogen to remain in the stream. The coupling of paraffinic components out of the lube boiling range would, in this case, increase lube yield and for this reason may represent a preferred process configuration. 
     The reaction between the lubricant component and the peroxide is carried out at elevated temperature, suitably at temperatures from about 50° C. to about 300° C. and in most cases from 100° C. to about 200° C. The treatment duration will normally be from about 1 hour to 6 hours but there is no fixed duration since various starting materials will vary in their reactivity and amenability to coupling by this method. The pressure employed will depend upon the temperature used and upon the reactants and, in most cases, needs to be sufficient only to maintain the reactants in the liquid phase during the course of the reaction. Space velocity in continuous operation will normally be from 0.25 to 5.0 LHSV (hr -1 ). 
     The peroxide is converted during the reaction primarily to an alcohol whose boiling point will depend upon the identity of the selected peroxide. This alcohol by-product may be removed during the course of the reaction by simple choice of temperature and pressure and accordingly temperature and pressure may be selected together to ensure removal of this by product. The alcohol may be converted back to the peroxide in an external regeneration step and recycled for further use. If ditertiary butyl peroxide is used, the tertiary butyl alcohol formed may be used directly as a gasoline octane improver or, alteratively, it may be readily converted back to the original di-tertiary butyl peroxide by reaction with butyl hydro-peroxide in the presence of a mineral acid, as described in U.S. Pat. No. 2,862,973, with the butyl hydroperoxide being obtained by the direct oxidation of isobutane, as described in U.S. Pat. No. 2,862,973. 
     The reaction may be carried out batchwise of continuously and in either case it is preferable to inject the peroxide compound incrementally so as to avoid exotherms and the production of lower quality products associated with high reaction temperatures. If the reaction is carried out in a continuous tubular reactor it is preferred to inject the peroxide compound at a number of points along the reactor to achieve the desired incremental addition. 
     The effect of the peroxide treatment is principally to increase the viscosity of the lubricant without affecting a significant reduction in viscosity index or significant increases in pour point or cloud point. The increase in viscosity implies an increase in molecular weight while the relatively constant pour point suggests that the reaction products are isoparaffinic in nature. It is thought that the action of the peroxide is by the removal of hydrogen atoms to form free radicals in non-terminal positions which then combine with each other to form branched chain dimers which are capable of reacting even more rapidly than the monomer. Thus, the viscosity of the treated material increases rapidly in the presence of additional amount of peroxide which generate new free radicals. The greater reactivity perceived with the initial dimer may be attributed to reactive tertiary hydrogen which are present in the dimers and higher reaction products but not on the paraffins present in the starting material. The greater reactivity of the dimers indicates that the incremental addition of successively smaller amounts of peroxide, particularly in continuous tubular reactor synthesis, will produce relatively greater progressive increases in viscosity and will also ensure that the range of molecular weights in the product will be narrower and that product quality will be more consistent. 
     The coupled products may include very small amounts of olefins and in order to improve the stability of the final lube products, the peroxide-treated products may be subjected to mild hydrotreating to saturate any lube range olefins. Treatment over a conventional hydrotreating catalyst such as Co/Mo on alumina at mild temperatures typically to 500° F. (260° C.) at relatively low hydrogen pressures, typically up to 1000 psig (7000 kPa) will normally be satisfactory. At low hydrotreat temperature up to about 550° F. (290° C.) viscosity loss on hydrotreating is minimal although greater losses maybe observed at higher temperatures. Pour point and V.I. remain relatively constant with temperature. 
     Because the peroxide treatment increases the molecular weight of the hydrocarbons by a coupling reaction resulting mostly in the production of dimers with some trimer and higher reaction products, the boiling point of the product increases commensurately with the extent of the coupling reaction. It is therefore possible to employ a non-lube fraction as the feed for the peroxide treatement step i.e. a feed boiling below the lube boiling range, for example, a 600° F.- about 315° C.-) fraction, especially the middle distillate boiling in the range of about 330°-650° F. (about 165°-345° C.). Fractions boiling below about 330° F. (about 165° C.) will normally not be preferred because excessive peroxide consumption is necessary to bring these naphtha range materials into the lube boiling range. 
     The peroxide treatment may be carried out before or after the hydrotreatment. Because the effluent from a catalytic dewaxing step may be cascaded directly to the hydrotreating step and from there to the peroxide treatment, this may represent an attractive processing scheme. Conversely, the use of a hydrotreatment step after the peroxide treatment may be desirable to remove residual unsaturation, as described above, and to reduce product bromine numbers to zero or to very low levels e.g. below 1.0. Another option is to carry out solvent extraction with furfural or another solvent after the peroxide treatment in order to remove any residual peroxide compounds or reaction by-products. This post-peroxide solvent extraction may be an additional extraction step or it may be the sole extractions step. Another alternative is to have the furfural extraction follow the dewaxing since both dewaxing and aromatics extraction may be favored by this sequence. The present processing scheme therefore provides great flexibility of operation in that the required steps may be carried out in various orders. The essential steps are the aromatics extraction, the dewaxing, the hydrotreating and the peroxide treatment all of which have a distinct function and purpose in the entire processing scheme and which may, as described above, be used in various sequences. 
     Very low pour point turbine oils may be produced by a second dewaxing step after the peroxide treatment (and after any subsequent hydrotreatment). The pour point of such products will typically be below -10° F. (-23° C.) and may be at least as low as -40° F. (-40° C.), comparable to those of synthetic lubricants. 
     EXAMPLE 1 
     This example illustrates the effects of solvent extraction, solvent dewaxing and hydrotreating on a neutral lube fraction. 
     The vacuum distillate was obtained from Arab Light Crude amounting to 6.6 volume percent of the crude and had the properties set out in Table 1 below: 
     
                       TABLE 1                                                     
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Arab Light Neutral                                                        
Gravity, °API   22.0                                               
Gravity, Specific      0.9218                                             
Pour Point, °F. (°C.)                                       
                       +90 (32)                                           
K.V. @ 100° C., cs                                                 
                       8.88                                               
Sulfur, wt. %          2.22                                               
Distillation, °F. (D-1160)                                         
1%                     705                                                
5%                     774                                                
10%                    789                                                
30%                    823                                                
50%                    856                                                
70%                    902                                                
90%                    949                                                
95%                    965                                                
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     The distillate was extracted with furfural conditions: 245% dosage, 120°/107°/100° C. Top/Feed/Bottoms temperatures) and then solvent dewaxed (conditions: 65/35 MEK/Toluene solvent, 160% dilution, 150% washing at a filtration temperature of -16° C.) to give a 37.3 vol. % yield of dewaxed oil based on raw distillate. The dewaxed oil was then hydrotreated over a Co/Mo/Al 2  O 3  catalyst at 2000 psig, 0.3 LHSV, 670° F., yield 94.5 vol. pct. (13890 kPa abs., 0.3 hr -   LHSV, .354° C., 94.5 vol. pct). 
     
                       TABLE 2                                                     
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Dewaxed AL Neutral                                                        
             Before     After                                             
             Hydrotreating                                                
                        Hydrotreating                                     
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Gravity, °API                                                      
               30.0         34.0                                          
Gravity, Specific                                                         
               0.8702       0.8550                                        
Pour Point     +10 (-12)    +15 (-9)                                      
Sulfur, wt. %  0.60         less than 0.01                                
Nitrogen, ppm  52           3                                             
Aromatics, wt. %                                                          
               25.9         4.4                                           
K.V. @ 40° C., cs                                                  
               54.02        32.04                                         
K.V. @ 100° C., cs                                                 
               7.61         5.71                                          
SUS @ 100° F. (38° C.)                                      
               279          165                                           
SUS @ 210° F. (99° C.)                                      
               51.7         45.4                                          
Viscosity Index                                                           
               103.4        119.8                                         
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     Hydrotreating removed essentially all the sulfur and nitrogen and saturated most of the aromatics, resulting in a much lower viscosity but also higher viscosity index. 
     EXAMPLE 2 
     This example illustrates the effect of peroxide treatment on the hydrotreated oil. 
     In each run of this Example, 100 g of the hydrotreated stock from Example 1 was placed in a 500 ml round bottom flask equipped with a stirrer, thermometer, water condenser, condenser liquid take-off and dropping burette. The flask was heated to 150° C., and the DIBP added dropwise from the burette over a one hour period. The temperature was held at 150° C. for a one hour period. The temperature was held at 150° C. for an additional three hours, then raised to about 185° C. in the next two hours. The contents were then cooled to room temperature and topped, first at atmospheric pressure to a pot temperature of 190° C. to improve any DIBP decomposition products not condensed in the take-off during the reaction period. 
     Three quantities of DIBP were used with results as set out in Table 3. 
     
                                           TABLE 3                                 
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DTBP Treatment Of Hydrotreated Oil                                        
Run                                                                       
No.         Charge                                                        
                  2-1   2-2   2-3                                         
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Stock, g          100   100   100                                         
DTBP, g           5     10    20                                          
Lube Yield, Wt. % 98.6  98.5  98.8                                        
Lube Properties                                                           
Gravity, °API                                                      
            34.0  33.1  32.6  31.5                                        
Specific    0.8550                                                        
                  0.8597                                                  
                        0.8623                                            
                              0.8681                                      
Pour Point, °F. (°C.)                                       
            +15 (-9)                                                      
                  +15 (-9)                                                
                        +10 (-12)                                         
                              +10 (-12)                                   
K.V. @ 40° C., cs                                                  
            32.04 45.50 59.24 93.54                                       
K.V. @ 100° C., cs                                                 
            5.71  7.20  8.66  11.88                                       
SUS @ 100° F. (38° C.)                                      
            165   234   305   484                                         
@ 210° F. (99° C.)                                          
            45.4  50.3  55.4  107.2                                       
Vis. Index  119.8 118.8 120.0 117.9                                       
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     The data show an increase in viscosity with essentially no change in pour point or viscosity indices. They also show that reaction with about 5% DIBP restores the viscosity to that of the dewaxed stock before hydrotreating. 
     EXAMPLE 3 
     This Example illustrates the effect of progressive addition of the peroxide compound. 
     In this Example, 50 g of the product from Run No. 2-2 of Example 2 was reacted with 5 g DIBP, effecting a second pass operation for comparison with Run 2-3 which used the same overall wt. % of DIBP in a single pass operation. Results compare as shown in Table 4. 
     
                       TABLE 4                                                     
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Multi-Pass DTBP Treatment                                                 
Run No.                  2-3       3-1                                    
Type           Charge    One-Pass  Two-Pass                               
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Gravity, °API                                                      
               34.0      31.5      30.7                                   
Specific       0.8550    0.8681    0.8724                                 
Pour Point, °F. (°C.)                                       
               +15 (-9)  +10 (-12) +10 (-12)                              
K.V. @ 40° C., cs                                                  
               32.04     93.54     114.4                                  
K.V. @ 100° C., cs                                                 
               5.71      11.88     13.94                                  
SUS @ 100° F. (38° C.)                                      
               165       484       593                                    
SUS @ 210° F. (99° C.)                                      
               45.4      67.2      75.3                                   
Vis. Index     119.8     117.9     121.3                                  
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     The two pass operation is thus more effective for increasing viscosity than the single pass. 
     EXAMPLE 4 
     This Example illustrates the effect of peroxide treatment before hydrofinishing. 
     The oil feed was the dewaxed Arab Light neutral of Example 1 before hydrotreating (Table 2 - before hydrotreating). 
     The oil (100 g) was reacted with DIBP (10 g) as described in Example 2, with the results set out in Table 5. 
     
                       TABLE 5                                                     
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DTBP Treatment of Dewaxed AL Neutral                                      
                Charge    Product                                         
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Yield, wt. %      --          99.5                                        
Gravity, °API                                                      
                  30.0        28.5                                        
Specific          0.8702      0.8844                                      
Pour Point, ° F. (°C.)                                      
                  +10 (-12)   +10 (-12)                                   
K.V. @ 40° C., cs                                                  
                  54.02       110.5                                       
K.V. @ 100° C., cs                                                 
                  7.606       12.48                                       
SUS @ 100° F. (38° C.)                                      
                  279         576                                         
SUS @ 210° F. (99° C.)                                      
                  51.7        69.5                                        
Vis. Index        103.4       104.5                                       
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     The results show that the hydrotreat step, removing essentially all the sulfur and nitrogen and saturating most of the aromatics, is necessary for the DIBP to be effective in increasing viscosity with no loss of V.I. or pour point. Thus the DIBP step can be used either after or before the hydrotreat step. 
     EXAMPLE 5 
     This example shows that the process of the present invention may be used to overcome the cloud point problem encountered with catalytically dewaxed oils. 
     The feed for these experiments was a catalytically dewaxed light neutral 318 stock having a +24° F. cloud point. This material had been solvent extracted (to remove aromatics) then catalytically dewaxed over ZSM-5. 
     Typical properties of a solvent dewaxed stock, at a 10° F. pour point, are a 17° F. cloud point, a viscosity of 34.8 CST at 40° C., 5.78 CST at 100° C., 180 SUS at 100° F., and a 107 VI. 
     The catalytically dewaxed stocks, used in the experiment reported below, are preferred because catalytic dewaxing is much more energy deficient than solvent dewaxing. The catalytically dewaxed material has a higher cloud point than desired (24° F. and a somewhat lower viscosity index (95) as compared to solvent dewaxed stocks. As reported in the following table, the peroxide treatment of the present invention eliminates the cloud point problem, increases the viscosity of the oil being treated, and brings about some improvement in viscosity index. For comparison purposes, the properties of atypical bright stock, BS 345, are also presented in Table 6. 
     
                       TABLE 6                                                     
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Bright Stock Production From Light Neutral                                
Using Free Radical Chemistry                                              
          FEED   INVENTION   Typical BS 345                               
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DTBP, wt. % 0        10      20    --                                     
Lube Properties                                                           
Pour Point, °F.                                                    
            10       5       0     20                                     
Cloud Point, °F.                                                   
            24       10      -6    36                                     
KV @ 40° C., cSt                                                   
            41.64    95.31   441.4 512.8                                  
100° C., cSt                                                       
            6.218    10.88   31.42 32.60                                  
SUS @ 100° F.                                                      
            215      497     2354  2755                                   
VI          95       98      102   95                                     
Flash Point COC, F                                                        
            439      --      460   --                                     
Bromine No. 1.0      --      1.9   --                                     
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     Table 6 shows that the peroxide treatment of the invention allows production of a lube stock from a light neutral with a viscosity approaching that of bright stock. The peroxide treatment also drastically reduces the cloud point, both in absolute terms and relative to the pour point. 
     The 30° F. drop in cloud point, resulting in a cloud point below the pour point, was unexpected.